Desalination of saline water by phase separation near critical pressure of pure water



July 28, 1970 A. O'SDOR 3,522,152

DESALINATION OF SALINE WATER BY PHASE SEPARATION NEAR CRITICAL PRESSURE 0F PURE WATER Filed April 20. 1964 I s Shets-Sheet 1 HEAT I/QCHA/VGEAS CH1 (PHHSE sm/eHr/ H are 71 SHl/A/f k/flTf/i" v Q /n/ 67/ (/1 CM 2 a P 'w Z fBR/NE COMPRESSOR NITROGEN PnRnrF/N A M. UCLA PURE WHTE/Q TURB/N' m FOR WORK our 'fi lwi WORK OUT i L".\\ A rm n/nrm x F4-. LF/

HX4 HX3 TU Z HEAT 7 exam/mam INVENTOR I ASRIEL OSDOR ATTORNEY July 28, 1970 A. OSDOR 3,522,152

DESALINATION OF SALINE WATER BY PHASE SEPARATION NEAR CRITICAL PRESSURE OF PURE WATER Filed April 20, 1964 8 Sheets-Sheet 5 INVENTOR. A S R I EL OSDO R urea/vs July 28, 1970 A. OSDOR 3,522,152

DESALINATION OF SALINE WATER BY PHASE SEPARATION NEAR CRITICAL PRESSURE OF PURE WATER 8 Sheets-Sheet 5 Filed April 20, 1964 INVENTOR. A 5 R/E L 05 D OR ATTORNEY July 28, 1970 A. OSDOR 3,522,152 DESALINATION OF SALINE WATER BY PHASE SEPARATION NEAR CRITICAL PRESSURE 0F PURE WATER Filed April 20, 1964 8 Sheets-Sheet 6 I INVENTOR.

ASRIEL OSDOR dz ta/ ATTORNEY July 28, 1970 A. OSDOR 3,522,152 DESALINATION OF SALINE WATER BY PHASE SEPARATION NEAR CRITICAL PRESSURE 0F PURE WATER Filed April 20, 1964 I 8 Sheets-Sheet 7 W0 FW/ Fig.6

INVENTOR ASRIE' L 05 DOR ATT/5% July 28, 1970 A. OSDOR 3,52

DESALINATIQN 0F SALINE WATER BY PHASE SEPARATION NEAR CRITICAL PRESSURE 0F PURE WATER Filed April 20, 1964 8 Sheets-Sheet 8 I NVEN TOR.

A SR/EL 0500/? BY 41; 4/ ATTORNEY United States Patent 3,522,152 DESALINATION 0F SALlNE WATER RY PHASE SEPARATION NEAR CRITICAL PRESSURE 0F PURE WATER Asriel Osdor, Tel Aviv, Israel, assignor, by mesne assignments, to Hydro Chemical 8: Mineral Corp., New York, N.Y., a corporation of Delaware Continuation-impart of application Ser. No. 89,099, Feb. 10, 1961. This application Apr. 20, 1964, Ser. No. 360,813 Claims priority, application Israel, Feb. 29, 1960, 13,557; Feb. 10, 1964, 20,773 Int. Cl. B01d 3/10; C02b 1/06 U.S. Cl. 203-11 8 Claims ABSTRACT OF THE DISCLOSURE A process and apparatus are described for the desalination of saline water by effecting the phase separation in the vicinity of the critical pressure of pure water, additionally compressing the pure water vapor, and utilizing the water vapor to heat raw saline water by countercurrent heat exchange. Intermediary fluids are used as heat-exchange media between the cold saline water and the hot pure water and vapor. One intermediary fluid is a gas (e.g. nitrogen) which is compressed while at a lower temperature and is expanded while at a higher temperature to generate an excess of work which is available for use in mechanically driving the fluids or for other purposes. Hydraulic pressure-exchanging devices are provided for driving, pumping or exchanging pressures between diiferent fluids in the process.

The present invention relates to a process and apparatus for separating solvents and/or solutes from liquid solutions, and to hydraulic pressure-exchanging devices useful therein. The invention can be advantageously used for producing pure or reduced-concentration solvents and/or pure or high-concentration solutes, as desired. It is particularly suitable for the demineralization or desalination of saline water, especially sea water, and is therefore hereinafter described with respect to this ap plication.

The present patent application is a continuation-in-part of my pending U.S. patent application Ser. No. 89,099 filed Feb. 10, 1961, now abandoned.

(A) INTRODUCTION Many systems have been heretofore proposed for desalinating saline water. However, the cost for desalinated water still remains very high because the known systems are generally characterized by relatively large initial equipment costs, large energy costs, and/0r large amortization and maintenance costs, for one or more of the following reasons: (1) requirement for a large amount of energy because of the latent heat of vaporization or freezing of water; (2) formation of corrosion and scale; (3) requirement for large size mechanical driving means for pumping, compressing, etc. the various materials involved.

An object of the present invention is to provide a new method and apparatus for the separation of a solvent and/ or solute from a liquid solution, and more particularly for the desalination of saline water, which method and apparatus have improved characteristics in one or more of the above respects.

A further object of the invention is to provide a method and apparatus for separating a solvent and/or solute from a liquid solution in which there is produced, as a by-product, an excess of energy available for mechanical Work, such as pumping or compressing the various 3,522,152 Patented July 28, 1970 fluids in the system, thereby substantially reducing or eliminating the need for relatively large and expensive mechanical equipment.

A further object of the invention is to provide novel hydraulic devices which translate or exchange the pressure of one fluid in the system to that of another fluid (which may be the same fluid under different conditions) in the system, the use of such devices further reducing the need for relatively large, expensive and corrosive-prone pumping, compressing and other mechanical equipment.

A number of additional objects and advantages of the invention will become apparent as the description proceeds, and are summarized at the end.

In the drawings:

FIG. 1a is a simplified diagram illustrating several features of the invention;

FIG. lb is a temperature-entropy diagram for pure water which will be helpful in explaining the invention;

FIGS. 2a and 2b, taken together, constitute a diagram of one design of water desalination system constructed in accordance with the invention;

FIG. 3 is a diagram of an improved design of water desalination system constructed in accordance with the invention;

FIG. 4 is a diagram of one form of hydraulic pressureexchanging device used in the system of FIG. 3;

FIG. 5 is another form of hydraulic pressure-exchanging device used in the system of FIG. 3;

FIG. 6 is a further form of hydraulic pressure-exchanging device used in. the system of FIG. 3; and

FIG. 7 is a diagram of an arrangement for pumping the incoming saline water into the system of FIG. 3 and for recovering the nitrogen used in the system.

The type of water desalination system in which the invention may be particularly used is that based on phase separation in the vicinity of the critical pressure.

The thermodynamic properties of pure water at the critical point are:

TABLE 1 Temperature374.15 C. Pressure225.65 kg./cm. Specific volume-0.00326 m. /kg. Enthalpy50l.5 kcal. Evaporation heat0 Entropyl.053 kcal./ C.

Phase separation at this point is based on the advantage that the latent heat of evaporation of pure water at or above the critical pressure is zero. However, it introduces another problem, called the squeeze problem in the discussion of this point by Ellis in his book Fresh Water From the Oceans, 1954, pp. 143151.

Briefly, the squeeze problem arises because of the following phenomenon. At the critical pressure (225.65 kg./cm. the specific heat of Water is approximately 1 kcal./kg. between 0 C. and C. and increases slowly to about 1.2 kcal./kg. at 300 C., and then rapidly to a mean specific heat of about 16 kcal./ C. between 370 and 380 C. The critical temperature of water is 374.15 C. Above the critical temperature, the specific heat of water decreases with further rise of temperature. Therefore, when using the separated vapor and brine fractions at'a temperature above the critical point to heat the cold saline water, they cannot provide the necessary heat for heating the saline water in the region of the critical point to raise its temperature the same number of degrees as the former are cooled. For example, cooling the vapor and brine 5 will not raise the temperature of the saline water 5. Much more heat must be added because of the increase of the specific heat at this point. This requirement for the greater amount of heat that must be added offsets to a substantial extent the gain that would otherwise be available from the fact that critical pressure distillation of pure water does not involve latent heat of evaporation.

To overcome the squeeze problem, it has been suggested (see Von Platen US. Pat. No. 2,520,186) to work at a pressure exceeding considerably the critical pressure, e.g. at pressures of about 300-350 kg./cm. However, this does not completely solve the squeeze problem. For example, at 300 kg./cm. there is still a squeeze area between about 395 C. and 405 0., wherein the mean specific heat is about 6.2 kcal./ C. Moreover, there are further draw-backs to this approach when used in desalination systems, including the following:

There are at least two important advantages both of which are lost in the above-suggested process, in efiecting the phase separation as near as possible to the critical pressure, or even a little below: namely, (1) it permits the use of less expensive equipment; and (2) it permits the production of desalinated water having a very low salt content. With respect to the latter, see The Phase Diagram of Sodium Chloride and Steam Above the Critical Point by Arne O'lander and Halvard Liander, ACTA Chemica Scandinavia 4 (1950) 14371445. The following table gives the phase separation temperature at the critical pressure for different sodium chloride concentration as abstracted from this diagram. It also gives the corresponding quantities of the liquid and vapor phases per 1036 kg. of a salt solution containing 3.5% sodium chloride, and the quantity of vapor separated by the rise in temperature.

TABLE 2 Vapor phase Sodium chloride Phase sepa- Liquid Vapor separated by concentration ration temphase phase rise in tem- (percent) perature 0.) (kg) (kg) perature (kg) 1 36 kg. salt.

TABLE 3.-CHLO RINE IONS CONCENTRATION OF THE SUPE RHEAIED VAPOR PHASE (PERCENT) Pressure (kg/MIL Temperature C.) 200 225 300 According to one feature of the invention the squeeze problem is largely avoided in the present process by effecting the phase separation in the vicinity of the critical pressure of the solvent; and then after phase separation, additionally compressing the solvent-rich vapor fraction to raise its specific heat before utilizing the heat of the solvent-rich vapor fraction to heat additional liquid solution to be desalinated. Because the phase separation is effected in the vicinity of the critical pressure, rather than at the considerably higher pressures previously suggested, the process may be used to produce desalinated Water of very low salt content, and moreover may be practiced with less expensive equipment. At the same time, the squeeze problem discussed in Ellis is largely avoided, as will be explained more fully below in connection with the description of the FIG. 1 diagram.

According to another feature of the invention, intermediary fluids are used as heat-exchange media between the cold raw liquid solution (saline water) and the hot solvent-rich fraction (substantially pure water). The inter- 4 mediary fluids are immiscible and chemically inert with respect to saline water and pure water and have a markedly higher or lower density than the water. Preferably, there are a plurality of heat-exchange cycles with the intermediary fluids coming into direct contact with the media being heated or cooled thereby.

In accordance with a further feature of the invention, the cold liquid solution is heated from the hot separated solvent fraction by means of at least one heat-exchange cycle which includes a gas intermediary fluid. The gas, during the heat-exchange cycle, is compressed while at a lower temperature and is expanded while at a higher temperature to generate an excess of work which is available for use in mechanically driving the fluids in the process, or for other purposes. The system thus converts thermal energy into mechanical Work needed to operate the plant, so that instead of supplying the expensive mechanical power, the much less expensive fuel heat may be supplied utilizing the thermodynamic cycle of the intermediary heat-exchange gas to generate the needed mechanical power as a byproduct of the process.

The foregoing features are schematically illustrated in the simplified diagram of FIG. 1a. In this diagram there are shown two heat-exchanging cycles using intermediary fluids, namely a cycle of nitrogen involving heat-exchangers HXl and HX4 and a paraflin (or other hydrocarbon) cycle involving heat-exchangers HX2 and HX3. As shown in FIG. 1a, the cold saline water is passed through a pump CM1 where its pressure is raised to the vicinity of the critical point of pure water, and then through heat-exchangers HXl and HXZ where its temperature is raised by hot nitrogen and then by hot paraflin. Further heat is added by heater Z, and phase separation occurs in phaseseparator PS, the brine exiting from the bottom. The pure water vapor is passed through compressor CM2 where its pressure is further raised, and the compressed water vapor is passed through heat-exchanger HX3 to heat the paraffin in the parafiin cycle. The water, now liquid, is passed through heat-exchanger HX4 to heat the nitrogen in the nitrogen cycle. The cold nitrogen exiting from heatexchanger HXI is passed through a compressor 0M3 where its pressure is raised before introduction into heatexchanger HX4, and the hot nitrogen exiting from the latter heat exchanger is passed through a turbine TUl where its pressure is dropped before introduction into heat-exchanger HXl. Turbine TUl produces work output which may be used for driving the fluids in the process, or for other purposes. The pure water exiting from heatexchanger HX4 is under high pressure which also may be used, as schematically shown by turbine TUZ, for producing work output.

According to a still further feature of the invention, hydraulic pressure-exchanging devices are provided for driving, pumping, or exchanging pressures between different fluids in the process. The use of such devices not only reduces the need for expensive mechanical motive power, pumping, compressing and fluid moving equipment, but also reduces or eliminates the need for moving parts coming into contact with the corrosive saline water.

(B) THE TEMPERATURE-EN'IROPY DIAGRAM OF FIG. lb

As indicated earlier, the squeeze problem is largely avoided according to a feature of the present invention involving the step of additionally compressing the solventrich vapor fraction after phase-separation in the vicinity of the critical pressure and before it is used to heat additional liquid solution to be demineralized. The results of the additional compression of the vapor phase are:

(l) A rise in the temperature of the vapor. For example, compressing adiabatically super-heated steam at 400 C. from 225 to 260 kg./cm. raises the temperature to about 421 C.

(2) An increase in the specific heat of the additionally compressed vapor. Consequently, in contrast to the very large temperature differentials (which means a very large amount of heat that had to be supplied at the top of the ladder to maintain a suflicient temperature differential in the vicinity of the critical point) required in previously proposed systems, a relatively small temperature differential between the two fluids at the top of the temperature ladder will be sufficient for a continuous heat transfer from the outflowing hot vapor at the higher pressure to the incoming raw liquid solution at the lower pressure.

The foregoing will perhaps be better understood by reference to FIG. lb which illustrates a temperatureentropy diagram for pure water.

In accordance with the preferred embodiment of the invention illustrated in FIG. 3, the phase separation is effected in the vicinity of the critical pressure in two successive steps, one step being at a temperature below the saturation temperature of the solution, and the other step being at a temperature slightly above. In this embodiment the first step of the phase separation is effected at say 400 C. (it may vary) in heat-exchanger H2 to be described, and the second step is effected at approximately 432 C., in tank S1 to be described. The saturation temperature of a sodium-chloride-water solution is approximately 428 C. at the critical pressure, saline water including other salts having of course a slightly diiIerent saturation temperature.

The temperature-entropy diagram of FIG. 1b is based on separating at a pressure of about 225 kg./cm. (as in the embodiment of FIG. 3), but additionally compressing the water vapor to a pressure of about 260 kg./cm. whereas the embodiment described in FIG. 3 compresses it to about 245 kg./cm. (In the FIG. 3 embodiment, a larger quantity of energy in the form of heat is supplied for the purpose of producing a mechanical work output, which accounts for the lower pressure.) Accordingly, although the pressures are not exactly alike between the diagram and the FIG. 3 embodiment, nevertheless the diagram will be helpful in explaining what happens and how the squeeze problem is avoided in the systems of both FIGS. 2 and 3.

In the diagram of FIG. 1b, curve A represents the temperature-entropy relationship of pure water at the critical pressure (about 225 kg./cm. and curve A represents this relationship at the higher pressure of about 260 kg./cm. Curve B is the vapor saturation curve. The diagram is arbitrarily cut horizontally at the temperature levels of 350 C. (623 A.) and -l53 C. (120 A.).

The point al on the critical pressure curve A corresponds to the ordinate T=380 C. (643 A.) and to the abscissa S=0.9628 kcal./kg. C. The point a2 on curve A corresponds to the ordinate T=380 C. (653 A.) and to the abscissa S:l.2037 kcal./kg. C. The shaded area below the points between all and a2 of curve A equals the amount of heat Q needed to raise the temperature of pure water fro-m 370 C. to 380 C. at the critical pressure. This amount of heat is obtained from the formula Q f T or from the steam tables, it is 155.8 kcal./kg. This is the squeeze area referred to earlier.

In the example described, phase separation is completed at about 432 C. This point is indicated as a3 in curve A. For the purpose of this examination it will be assumed that the water vapor alone is used to heat the saline water to the phase separation temperature, and that the water vapor must always be at a temperature differential of at least C. to provide the proper heatexchange relationship between the two media.

In the conventional critical pressure phase separation system, the water vapor would have to be heated from 432 C. (point 03) to a point on curve A where the area underneath the curve between the two points equals the area unlerneath curve A between points a1 and a2, i.e. the squeeze area. Disregarding the heat losses, this point would be 613 C. (886 A.), which is indicated on curve A by the reference a4, the shaded area between points a3 and a4 equaling the shaded area between points a1 and a2. Thus, the water vapor would have to be heated almost 200 C. above the phase separation temperature, to maintain a temperature difierential of 10 C. at the squeeze region, which heretofore made this system impractical for water desalination on any large commercial scale.

By the additional compression, however, the water vapor is compressed raising the temperature to point a4 on curve A, in this example about 456 C. If the water vapor were now used to heat the saline water, its cooling path would pass down along curve A, the temperature differential (starting at 456 C.432 C.) decreasing until a point is reached, called a'2, Where it is to be 10 over 370 C., the bottom of the squeeze, i.e. a2 equals 380 C. Another point a1 is marked where the ordinate of this point intersects curve A.

Since the amount of heat transferred from the water vapor equals the amount of heat received by the saline water, the area underlying curve A between points a1 and a3 must equal the area underlying curve A between points a2 and a4. In this case, Where the water vapor is compressed from 225 kg./cm. to 260 kg./cm. this cannot be attained without additional energy input. Accordingly, the water vapor, after the compression, is heated (as by heating coil F1 in FIG. 3) to increase its temperature to point a"4 on curve A. The amount of additional heat necessary is such that a4 will be at the point where the area underlying curve A between points a1 and a3 will equal the area underlying curve A between points a'2 and a"4. This means that the area (double-shaded) underlying points (1'4 and a4 on curve A will equal the area (double-shaded) underlying points all and a1 on curve A, less the area between curves A and A from points a'2 and a4, and points a1 and a3.

In this example, the latter-mentioned area (representing a part of the energy by the additional compression) is about 6 kcal./kg., and the first-mentioned doubleshaded area (representing the energy by the additional heating) is about 7.9 l cal./ kg. Thus, by this additional compression which shifts the temperature-entropy relationship of the water vapor, only about 9.5 kcal./kg. of heat would have to be added in this example.

(C) COMPARISON WITH THE KNOWN VAPOR- COMPRESSION SYSTEM The above described process is to be clearly distinguished from the known vapor-compression method of distilling water, in which the vapor produced in the evaporator is compressed and the heat of its condensation is used as the heat supply to boil the solution in the same evaporator.

In the vapor-compression distillation system, the compressed vapor is condensed at a constant temperature along a horizontal temperature line (the condensation temperature of pure water), and similarly the saline water is vaporised at a constant temperature along a horizontal temperature line (the boiling temperature of the outflowing concentrated brine). The compressed vapor must be at a sufiiciently high temperature to maintain the required heat-exchange temperature differential With respect to the boiling temperature of the concentrated brine. This means that the compressed-vapor temperature must be at the heat-exchange temperature differential with respect to the boiling point of the highest concentration of saline water resulting from the distillation. For example, if of the pure water is to be separated from the saline water, the resulting concentration of saline water would have a boiling point of about 108 C. at atmospheric pressure. Assuming a 5 C. heat-exchange temperature differential, the compressed-vapor should have a temperature of about 113 C. Under these conditions, the work of adiabatic compression, at 100% efficiency, would be about 24 kwh. per 1,000 kg. of water vapor to be compressed from about 1 atmosphere (1.0332 kg./cm. to about 1 /2 atmospheres (1.6144 kg./cm.

In the present process, however, the compressed vapor follows a descending (not horizontal) temperature line as it cools, and the saline water being heated follows an ascending line, as described earlier with respect to FIG. 1 and as apparent from Table 2. It will also be noted that the former line is always higher (by at least 10 in the example described above), sufficiently to maintain the heatexchange temperature differential by the additional compression. The work of compression in this example, with a temperature differential of at least 10 C., would be about 10 kwh., at 100% efficiency.

Thus, in the present method about 10 kwh. of work would be needed for an output of 90100% of the pure water, while maintaining a temperature differential of 10 C.; whereas in the known vapor-compression system, about 24 kwh. of work would be needed for an output of about 90% of pure water, with a temperature differential of only 5 C.

There are further important differences, particularly when using intermediary fluids in the vapor-compression process as compared to using them in the present process. Since the condensation and boiling temperature curves of the compressed-Vapor and concentrated saline water, respectively, are substantially horizontal in the known vapor-compression method, a much larger quantity of intermediary fluid would be necessary than in the present invention wherein the temperature curves follow descending and ascending lines respectively. In the given example of utilizing compressed vapor at 113 C. to heat saline water at 108 C., there would be required about 534,000 kcal. per 1,000 kg. of pure water produced. Assuming the intermediary fluid is paraifin and that a mean temperature differential of about 2.5 C. is maintained between the paraffin and the condensing vapor on the one hand, and the boiling saline water on the other (the paraflin being heated from 110 to 111 C. and cooled from 111 to 110 C., respectively), about 1,000 m. (800 tons) of paraffin would be required per 1,000 kg. of pure water produced.

In the present process, where the cooling and heating temperature curves are in descending and ascending lines, respectively, counter-current heat-exchange may be continuously effected, and it is calculated that about m. of parafiin would be necessary per 1,000 kg. of pure water produced. The paraflin is heated and cooled by more than 100 C., respectively, in the examples of FIG. 2 and FIG. 3.

Still further, t he work of compressing the 1,000 m. of paraffin in the known vapor-compression method, from 1.0332 kg./cm. to 1.6144 kg./cm. would be about 16 kwh. for 100% efliciency. This work, as a practical matter, would be hardly possible to recover because of the small pressure differential (about one-half atmosphere). In the present process, however, the intermediary fluid (paraffin) is compressed more than 20 atmospheres in the examples described, and therefore the work invested in this compression may more easily be recovered and utilized during its expansion.

It has been further suggested (e.g. see Gilliland US. Pat. No. 2,976,224) to use, in a vapor-compression system, the heat from solidifying material to vaporize saline water and then to use the heat of condensation of the compressed water vapor for remelting the previously solidified material. Here, however, the volume of the circulating intermediary fluid is much larger than required in the present process, by to 90 times, depending on the molten material used.

For the foregoing reasons, vapor-compression systems have heretofore been attractive mostly for moderate size installations (e.g. shipboard), and have not been generally used for large size installations or Where it is critical to 8 produce pure water at the lowest possible cost. The sys tem of the present invention is believed capable of producing pure water at a fraction of the cost of vaporcompression systems.

As brought out earlier, the critical point of water is at a pressure of about 225 kcal./cm. (approximately) and at a temperature of about 374 C. (approximately). The critical points of saline Water are slightly higher. In the embodiments of the invention discussed above, i.e. with respect to FIG. 3, the phase separation is carried out at a pressure slightly above the critical pressure of 225 kg./ cm. and in two stages of temperatures, namely 400 C. and 432 C. In another embodiment, that of FIG. 2, the points are somewhat different, being at about 227 kg./ cm. with one phase separation temperature being at about 395 C. and with the highest temperature being about 410 C. In any event, it is not essential that phase separation be conducted at exactly these points to obtain the below-described advantages of the present invention. For example, a phase-separating temperature of about 364 C. and pressure of about 200 kg./cm. (193 atmospheres) could be used (the vapor being compressed to a higher pressure preferably above the critical pressure), but the efliciency of the process would be reduced by lowering the phase-separation pressure and temperature below the critical points. Operating at higher than the critical points will tend to increase the salinity of the produced water and the cost of the equipment, as discussed above.

Accordingly, when the term vicinity is used herein with respect to the expressions of critical point, critical pressure, and critical temperature, it will be understood to include not only the exact critical points, but also a little below or a little above them.

(D) THE HEAT-EXCHANGE MEDIA An important feature of the invention, as indicated earlier, is that intermediary fluids are used as heatexchange media between the cold saline water and the produced hot pure water (vapor and liquid) and hot saline brine, the fluids being practically immiscible, chemically inert, and of different density than the water. The heat exchangers may be upright cylindrical receptacles having a large diameter (e.g. 1 meter), wherein either hot or cold intermediary fluids flow (either freely or between morsels of coke, for instance, filling up the upright cylindrical receptacles) in counter-current heatexchange and in direct contact with the incoming cold saline water, or with the outflowing hot fresh water (vapor and liquid) and hot saline brine, respectively. There are no tubes within such a heatexchanger, so that there would be no problem of scale or corrosion.

Another form of direct-contact counter-current heatexchanger that may be used is that described in my US. patent application No. 346,953 filed Feb. 24, 1964, now abandoned.

Many fluids have the above-mentioned properties at determined temperature regions between the ordinary temperature and the critical temperature of the water, so that by forcing the saline water to flow through a series of upright tanks from bottom to top (or from top to bottom) and injecting into each one of the tanks at the top (or at the bottom, according to the density of the intermediate fluid), it is possible to heat the saline water gradually from ordinary temperature to above the critical temperature, while flowing from tank to tank through a series of tanks in counter-current to a series of fluids injected into the tanks, each one of the injected fluids being at a higher temperature than the preceding fluid in the series of fluids used.

The heat transfer in the described embodiments is carried out by two or more cycles of heating and cooling and also of compression and expansion of an intermediary fluid or fluids, each cycle being operated within a determined temperature region, the quantity of the fluid circulating per hour through each one of said cycles being equal to the quantity of saline water driven into the desalinization plant per hour, multiplied by the mean specific heat of the water, and divided by the mean specific heat of the intermediary fluid at the temperature region of each cycle, to provide substantial equalization of heat capacities.

Example 1 One example of an intermediary fluid is a liquid such as mercury or tars having a higher critical temperature than the critical temperature of the water and a lower vapor pressure at all temperatures, and having a greater density than the density of the water between the ordinary temperature and the highest temperature of the process.

Such a fluid could be used as an intermediary fluid in the region between ordinary temperature and above the critical temperature of water, i.e. at all the temperatures of the process. Mercury, for instance, is not miscible and does not react chemically with saline water. The small quantity of mercurous chloride that may be produced. within the heat-exchangers by chemical reaction between the saline water and the mercury vapor at high temperature and under high pressure could be separated from the other precipitated salts by sublimation, and the mercury could thus be regenerated.

The specific heat of mercury between ordinary temperature and the highest temperature of the process (e.g. in the FIG. 2 embodiment) is approximately 0.033 kcal./kg. This material could be used in the process as the heat transfer medium by operating three mercury cycles per 1000 liters of saline water driven into the desalinization plant per hour, as follows: a first cycle of about 30 tons of mercury (about 2.3 m. per hour in the region 19 C. 200 C.; a second cycle of about 40 tons of mercury (about 3.1 m in the region 200 C.- 345 C., and a third cycle of about 90 tons of mercury (about 7 ms") in the region 345 C.403 C.

For example, 1000 liters of saline water at 17 C., are compressed from 1 to 220 atmospheres (1.033 to 227 kg./cm. and heated to about 196 C., by countercurrent heat-exchange with about 30 tons of mercury at 200 C. (the first mercury cyclesee above). Then the saline water is heated from 196 C. to about 335 C. by counter-current heat-exchange with about 40 tons of mercury at 345 C. (the second mercury cycle-see above). Then the saline water is heated from 335 C. to about 395 C. by about 90 tons of mercury at 403 C. (the third mercury cyclesee above).

By elevating the temperature of the saline water under the pressure of 220 atmospheres from 1 to 395 C., it expands from 1000 to about 7700 liters and could be separated, while flowing through a horizontal tank, into an upper light fraction (about 90% of the incoming saline water) containing less than 400 p.p.m. of salts (i.e. good fresh water), and a lower heavy fraction (about of the incoming saline water) of a concentrated saline brine. Finally the light fraction is submitted to further rise of temperature up to 410 C., for instance, by additional compression. Then both fractions separately (the light fraction at 410 C. and the heavy fraction at 395 C.) are cooled to about 350 C. by counter-current heat-exchange with about 81 tons of mercury at 345 C. for the fresh water, and about 9 tons of mercury at 345 C. for the saline brine, the mercury being thus heated to about 403 C. Then the fresh water and the saline brine are cooled to about 204 C. by counter-current heat exchange with about 36 tons and about 4 tons of mercury, respectively, at about 200 C., the mercury being thus heated to about 345 C. Finally the fresh water and saline brine are cooled from 204 C. to about 21 C. by counter-current heat-exchange with 27 tons and 3 tons of mercury respectively at about 19 C. The energy liberated by the cooled fresh water and saline brine, while expanding to 1 atmosphere before being evacuated from the plant, is used to return a substantial proportion of the work of compression supplied to the system.

Example 2 The intermediary fluid or fluids could be substances such as paraffin having a higher critical temperature than the critical temperature of the water and a lower vapor pressure at all temperatures, and having a smaller density than the density of the water at ordinary temperature. Such a fluid could be used as an intermediary fluid in the region between ordinary temperature and about 300 C. and also in the region above 350 C., for instance. At the lower temperature region the density of the water is higher than that of the paraffin, so that the water will flow from top to bottom of the heat exchanger in counter-current heat-exchange to the flowing-up paraffin. At the higher temperature region the density of the water is lower than that of the paraffin, so that the water will flow from bottom to top of the heat-exchanger in counter-current heat-exchange to the flowing-down paraflin.

Paraffin is more miscible in water at higher temperatures than at ordinary temperatures. However, the water is removed from the system at a few degrees above ordinary temperature, and therefore the paraflin contained in the water at the higher temperature may be easily separated at the lower temperature.

Example 3 Fluids in the gaseous state having a critical temperature below ordinary temperature (such as air, preferably nitrogen), not miscible with and chemically inert to water and saline water (especially sea water) in the temperature region between ordinary temperature and a little below the critical temperature of water, could be used as intermediary fluids in the region between ordinary temperature and a little below the critical temperature of the water.

In the following examples described with respect to both the FIGS. 2 and 3 embodiments, it is proposed to use compressed fluids in the gaseous state, preferably nitrogen, as the intermediary fluid for the heat-exchange between the incoming sea water and the outflowing desalinated water and saline brine in the region between ordinary temperature and a little below the critical temperature of the water; and to use fluids in the liquid state, such as paraffin, in the region between a little below the critical temperature to the highest temperature of the process. The former (the compressed gases or nitrogen) has a smaller density than the density of the water below its critical point, and the latter (the paraflin wax, for instance) has a greater density than the density of the water in the region 'between a little below the critical temperature of the water and the highest temperature of the process.

As indicated earlier, according to one feature of the present invention, the cycle of the gas or gases includes expansion of the same and converting into mechanical power a part of the thermal energy supplied to the system, thus producing all or most of the mechanical work needed to perform the cycles of the waters and of the intermediary fluids so that instead of using the very expensive mechanical power, the much cheaper fuel energy may be used.

(B) THE FIG. 2 EMBODIMENT FIG. 2 (i.e., FIGS. 2a and 2b taken together) is a diagrammatic showing, by way of example, of a plant for carrying out the invention, using successively nitrogen and paraflin as intermediary fluids, these having the required properties between ordinary temperature and the final temperature of the process.

The specific heat of the paraflin used in the following example is about 0.7 kcaL/kg. in the temperature region 1 l of 340440 C. and in the pressure region 220-245 atmospheres (227-253 kg./cm. and the specific heat of nitrogen is about 0.25 kcaL/kg. in the region of -350 C. and 220-245 atmospheres.

The plant illustrated in FIG. 2 comprises essentially a saline water cycle, a desalinated water cycle, a saline 'brine cycle, a paraffin cycle and a nitrogen cycle, including compressors, prime movers, pumps, heat exchangers, heating units, and saline water separators.

(1) Water and brine cycles.The saline water or sea water at ordinary temperature, for instance 17 C. (t flows into the plant through pipe 1, manifold 2, valves 3 or 3', and into a double-acting pump P having a cylinder 4 and a piston 5. The latter is positively reciprocated by means of piston rod 6 connected to piston 7 moving within cylinder 8 of prime mover M When the right cylinder chamber of pump P acts as delivery chamber, it is connected through a stop valve 9, manifold 10, conduit 11, and sprayer or distributor 12, with the top end of an upright heat exchanger hl. Here the saline water, which is compressed by pump P from 1 atmosphere to above the critical pressure (for instance to 220 atmospheres, the initial pressure of the system), is heated by counter-current heat exchange with hot nitrogen at a temperature of 363 C. (t for instance, and at a pressure of 220 atmospheres. The nitrogen is injected above the bottom of heat exchanger tank hl by means of injector a and flows up through heat exchanger tank h 1 in counter-current to the flowing down saline water.

The flowing-down saline water passes through funnel 13 into the conical cell 14, wherein are deposited and collected solid particles contained in or precipitated from the saline water. The deposited solids are evacuated from time to time, together with small quantities of saline water, by opening valve 15.

Then the sea water at a temperature of e.g. 356 C. (t flows through conduit 16, distributor 17, and through heatexchanger I12 (from bottom to top), and is heated to a temperature of e.g. 395 C. (t by counter-current heatexchange with paraffin at a temperature of about 407 C. (t and at 220 atmospheres pressure, injected by injector a at the top of heat exchanger I12.

The paraffin, cooled to e.g. 358 C. (r while flowing through heat-exchanger h2, passes through the funnel b into cell c, where solid particles precipitated from the sea water are deposited and collected. They are evacuated in the following manner, for example:

Valve G is closed and valves d and G are opened (valve G and G remaining closed). In this manner the deposited solids together with paraffin flow from cell c into tank E through valve d and conduit F. The solid particles are deposited at the conical bottom of tank E, and pure paraffin is passed through valve G by pump P (see below). Then valves G and G are opened and valve a is closed. Cold sea water at 220 atmospheres that flows through conduit 11', having a greater specific gravity than the specific gravity of the paraffin, is collected at the bottom of tank E, While pure paraffin forms an upper layer. Then valve G is opened and valve G is closed to evacuate the deposited solid particles together with a small quan tity of sea water. Finally by closing valves 6.; and G we return to the normal functioning of the apparatus.

Heat-exchanger h2 also serves as the main phase separation chamber or column, since at 220 atmospheres the phase separation of sea water, for instance, starts at about 378 C., and at 395 C. approximately 85% of the sea water is separated as practically pure water vapor from a residual brine containing approximately of dissolved salts (see Table 2 above).

The hot mixture of brine and water vapor flows out at the top of heat-exchanger h2 at a temperature of e.g. 395 C. (I or a little below, either through conduit 18 (in dotted lines) or through heating coil 19. This coil is heated by fuel heat (in addition to the heating of coils 19 and 19") with the purpose of raising the temperature of the 12 hot mixture of brine and vapor flowing into tank s and for starting the apparatus. The mixture of brine and vapor then passes through conduit 20, valve 21, and finally into the horizontal separator and settling tank s, flowing out separately at the bottom and at the top of its right end, through valves 42 and 26 respectively.

The hot water vapor at about 395 C. and at 220 atmospheres, having a specific volume of about 7.7 litres per kg., flows from right to left of tank s and is separated into an upper layer of water vapor poor in salts, and a denser lower layer of a brine containing in solution most of the salts of the treated saline water and in suspension the salts not separated in tank I12, and the salt crystals precipitating from the denser lower layer. These are deposited and collected in the conical cells 22, 23, to be evacuated together with a small quantity of the saline brine by opening from time to time the valves 24, 25, respectively.

At the upper and left end of tank s, desalinated Water (vapor) flows out (containing less than 0.04% of salts) through valve 26, conduit 27, manifold 28, and valve 29 or 29', into the cylinder of compressor 01. While desalinated water vapor flows into the left cylinder chamber of compressor 01 (having cylinder 30 and piston 31), the right cylinder chamber acts as delivery chamber wherein the water vapor is compressed from 220' to 245 atm. (i.e. 227 to 253 kg./cm. the highest pressure (ph) in the system of FIG. 2. This causes the elevation of its temperature from e.g. 395 C. to the highest temperature of the system, e.g. 410 (t This is the additional compression which avoids the squeeze problem as discussed above with respect to FIG. 1.

The highly compressed desalinated water (vapor) is delivered through valve 32, manifold 33, conduit 34, and distributor 35, into heat-exchanger I23 at its bottom. The hot desalinated water vapor at about 410 C. flows up from the bottom to the top of heat-exchanger 11 3 in counter-current to the flowing-clown paraflin injected at a temperature of e.g. 358 C. (t and at 245 atmospheres (253 kg./cm. through injector a';; (see below the paraflin cycle).

The desalinated water is cooled by counter-current heatexchange with the flowing down paraflin to a temperature of e.g. 370 C. (t It then flows through conduit 36 and distributor 37 into heat-exchanger h4 at its top, flowing down through this heat-exchanger from top to bottom in counter-current heat-exchange with the flowing up nitrogen. The latter is injected by injector a at a temperature of e.g. 28 C. and by injector a at e.g. 229 C. (i and at 245 atmospheres pressure (see below the cycle of the nitrogen).

The desalinated water at about 30 C. (t and 245 atmospheres flows out at the bottom of heat exchanger 114 through conduit 38, manifold 39, valve 40, and into the left cylinder of prime mover M driving from left to right the piston 7 which is connected by piston rod 6 to piston 5 of pump P In this manner the desalinated water at a temperature a little above ordinary temperature and under a pressure of 245 atmospheres, while flowing into the left cylinder chamber of prime mover M drives the cold saline water from the right cylinder chamber of pump P into the heat exchanger h1, wherein the pressure is only 220 atmospheres.

At the lower left end of tank s flows out the residual saline brine through the conical cell 41, valve 42, conduit 43, manifold 44, stop valves 45 or 45 and into reservoirs r1 or r'l. The latter are connected by the short tubes 46 or 46' with the left or the right cylinder chamber of compressor 02, respectively.

The cylinder 47 of the compressor 02 and the lowest part of the reservoirs 1'1 and r1 are filled with a liquid (for instance, paraflin wax) that is inert with respect to the compressor and is not miscible and does not react chemicaly with the saline brine. The pressure of the piston 48 of the compressor 02 on the inert liquid within the cylinder chamber is transmitted by this liquid to the saline brine within the reservoir, and vice versa. In this manner, contact between the corrosive hot saline brine and the cylinder and piston of the compressor c2 is avoided. The saline brine at a pressure of 220 atmospheres flows into reservoir r1, for instance, while the piston 48 drives out the inert fluid from the right cylinder chamber of the compressor c2 through pipe 46' into the reservoir r1. The inert fluid flowing into reservoir r1 compresses the saline brine Within the reservoir from 220 to 245 atmospheres and then drives out the compressed saline brine through stop valve 49', the reservoir r1 being filled up with the inert fluid when the piston 48 is at the right end of its course. When the piston 48 is at the left end of its course, the reservoir r1 is filled with the insert fluid, and at this moment the volume of the saline brine flowing into reservoir r1 at a pressure of 220 atmospheres is equal to the volume of the cylinder chamber of compressor c2.

If the intermediary fluid used is mercury or any other fluid that its contact with the pumps, compressors and prime movers of the apparatus should be avoided (even nitrogen containing small quantities of saline Water is dangerous to the compressors and prime movers), then to each one of them two reservoirs could be added and they could be operated in the manner described above. The two reservoirs would be placed above or below the pump, compressor or prime mover, if the intermediary fluid is lighter or heavier than the inert liquid used, re-, spectively.

The additionally compressed saline brine flows from reservoir r1 or r1 through stop valve 49 or 49', respectively, manifold 50, conduit 51 and injector 12 into heat exchanger I15 at its top. There it flows down in countercurrent to the flowing-up nitrogen injected by injector b at the bottom of the heat exchanger (at about 28 C., t by injector b at about one third of its height (at about 229 0., t and by injector b at about half of its height (at about 368 0., 1 The saline brine flows out at the bottom of heat exchanger h at a temperature of e.g. 30 C. (t through funnel 13', cell 14', conduit 52, manifold 53, valve 54, and into reservoir r2. It drives the inert fluid which is lighter than the saline brine through tube 55 into the left cylinder chamber of prime mover M the latter including cylinder 56 and piston 57 which is driven by the inert fluid from left to right. While the saline brine at a pressure of 245 atmospheres (253 kg./cm. flows into reservoir r2, the stop valve 58' is open, and the saline brine within the reservoir r2 flows out through valve 58, manifold 59 and conduit 60, at a pressure of one atmosphere. The work of expansion is utilized to help drive piston rod 6 connected to the pistons of the pumps, compressors and prime mover of the apparatus.

The cooled saline brine at a temperature of e.g. 30 C. (t flows out from reservoirs r2 or r2 of prime mover M through valve 58 or 58, manifold 59, and conduit 60 at a pressure of one atmosphere. The cooled fresh water at a temperature of e.g. 30 C. (i flows out from prime mover M through valve 61 or 61', manifold 62, and conduit 63, at a pressure of 1 atmosphere. The Work of expansion from 245 to 1 atmosphere is utilized in the plant by means of piston rod 6, for instance.

The precipitated salts within the conical cell 14' are evacuated together with a small quantity of saline brine by opening and closing valve 15'.

(2) Paraflin cycle.The cycle of paraflin is performed by means of prime mover M with cylinder 64 and piston 65 connected to piston rod 6.

For the heat exchange between about 1 ton of desalinated water vapor at about 410 C. and 1.1 ton of saline water at about 356 C. per second (or per minute, or per hour, for instance), a cycle of about 4.3 tons (about 6.5 cubic meters) or paraflin is performed per second (or per minute, or per hour respectively) in the following manner: The paraffin at 245 atmospheres and at e.g. 403 C. (r flows out at the bottom of heat exchangers 113 (see above) through conduits 66 and coil 19, where the flowing paraflin is heated by fuel heat to 407 C. (t' in addition to or instead of the heating of coil 19 (see above). It then flows through manifold 67, stop valve 68, into the left cylinder chamber of prime mover M driving piston 65 from left to right. At the same time the right cylinder chamber of prime mover M acts as a delivery chamber and is connected through stop valve 69, manifold 70, conduit 71, heating coil 19" and injector a3 with the top of heat exchanger h2. Here the paraffin, after expansion within the cylinder chamber of prime mover M from 245 to 220 atmospheres, is injected and then flows down through heat exchanger h2, in counter-current to the flowing-up sea water (see above). The flowing-down paraflin is cooled from e.g. 407 C. (t to e.g. 358 C. (t by the flowing-up saline water. The latter is injected through injector 17 and is heated from the temperature of e.g. 356 C. (t7) to e.g. 395 C.

The cooled parafiin flows through funnel b, cell c and valve G or through valve d, conduit F, cell E and valve G (see above), manifold 72, conduit 73, manifold 74, and valve 75, and then into the left cylinder chamber of pump P including cylinder 76 and piston 77 connected by piston rod 6 to piston 65 of prime mover M In this position, the right cylinder chamber, wherein the paraflin is compressed from 220 to 245 atmospheres, acts as delivery chamber and is connected through stop valve 78, manifold 79, conduit 80, and injector a3, with the top of heat exchanger k3. The injected paraifin flows down through the heat exchangers h3 and is heated from about 358 C (t to about 403 C. (t by countercurrent heat exchange with the flowing-up desalinated water (vapor) through heat exchanger h3, flowing in at the bottom of this heat exchanger at about 410 C. (t through distributor 35, and flowing out at e.g. 370 C. (t at the top through conduit 36 (see above). The heated paraffin at about 403 C. and 245 atmospheres flows out at the bottom of heat exchangers 113, thus completing one paraffin cycle and starting a new paraffin cycle.

Although the quantity of parafiin driving the piston 65 of prime mover M is the same as the quantity of paraffin driven by the piston 77 of pump P the volume of the latter at the same pressure of 245 atmospheres is smaller, because its temperature (about 358 C.) is about 45 C. lower. Consequently, the prime mover M produces theoretically more mechanical energy than the mechanical energy needed for the functioning of pump P per same cycle.

(3) Nitrogen cycle.--For the heat exchange between about 1 ton of desalinated water vapor and about 0.1 ton of saline brine and 1.1 ton of the incoming saline or sea water per unit time (per second, per minute, or per hour). a cycle of about 5.72 tons of nitrogen (100% of the nitrogen cycle) per unit time (per second, per minute, or per hour, respectively, is performed in the following manner: About 5.15 tons of nitrogen of the nitrogen cycle) at 245 atmospheres and at a temperature of e.g. 368 C. (r flow out at the top of heat exchanger 714 through conduit 81. It is injected through injector b at about one-half the height of heat exchanger h5 and flows up together With about 0.57 ton of nitrogen (about 10%) injected through injector b (about 7.7% or about 0.44 ton at about 28 C. (t and through injector b (about 2.3% or about 0.13 ton at about 229 C., t

The flowing-up 5.72 tons of nitrogen through heat exchanger 115 are heated from e.g. 368 C. to e.g. 378 C. by counter-current heat exchange with the flowing down kg. of saline brine at about 395 C. per cycle of 1.1 tons of incoming saline water. The 100 kg. of the saline brine are thus cooled from 395 C. to 370 C. supplying to the 5.72 tons of nitrogen about 14,000 kcal.

Now, these 14,000 kcal will be supplied to the hot saline water from an external source of energy (fuel heat, for instance), while flowing through the heating coils 19, 19 and 19 (see above).

The 5.72 tons of nitrogen flowing out of the top of heat exchanger h5 at about 378 C. (tiz) flows through conduit 82 and coil 83, where its temperature is elevated to 383 C. (1 'by supplying about 7,000 kcal. of fuel heat.

Assuming losses of heat by the heating, the total fuel heat supplied to coils 19, 19, 19" and 83 per 1000 litres of fresh water produced from 1100 litres of sea water is about 26,000 kcal., or about 30 kwh.

The nitrogen at 345 atmospheres and at 383 C. flows through conduit 84, manifold 85, stop valve 86 into the left cylinder chamber of prime mover M having cylinder 87 and piston 88. Here the nitrogen expands (adiabetic expansion) from 245 to 220 atmospheres, and is thus cooled to 363 C. (I At the same time the right cylinder chamber of prime mover M acts as a delivery chamber and is connected through stop valve 89, manifold 90, conduit 91, and injector a with the bottom of heat exchanger h. The nitrogen flows up through this heat exchanger in counter-current to the flowing down saline water (see above). The nitrogen is thus cooled to a temperature of e.g. 214 C. (1 at the level of tube a by the flowing-down saline water, the latter being heated from a temperature of e.g. 200 C. (2 at the level of tube a to a temperature of e.g. 356 C. (t at the bottom of heat exchanger hl.

About 23% or 1.32 tons per cycle of the total nitrogen injected at the bottom of heat exchanger 111 is intercepted and passes through tube a and the other 77% or 4.4 tons of the nitrogen per cycle continues to flow up through heat exchanger h1 in counter-current to the flowing-down saline water flowing into heat exchanger h1 through distributor 12 at ordinary temperature e.g. 17 C. (t The so cooled nitrogen flows out at the top of the heat exchanger hl at a temperature of e.g. 19 C. (t through conduit 92, manifold 93, stop valve 94, into the left cylinder chamber of compressor c3 (including cylinder 95 and piston 96) to be compressed adiabatically from 220 to 245 atmospheres. The temperature is raised by this compression from e.g. 19 C. (t to e.g. 28 C. The work of compression of the 77% of nitrogen (4.4 tons of nitrogen per cycle of 5.72 tons) is about 1.16 kwh. At the same time the right cylinder chamber of compressor (:3 acts as a delivery chamber and is connected through stop valve 97, manifold 98, conduit 99, regulating valve wl, conduit 100 and injector a' with heat exchanger [11 at its bottom and also through regulating valve w'1, conduit 100 and injector b with heat exchanger I15, at its bottom.

About 69.3% or about 3.96 tons of nitrogen per cycle flows through regulating valve w1, and about 7.7% or 16 about 0.44 ton of nitrogen per cycle flows through regulating valve w1.

After flowing up through heat exchanger k4 in countercurrent heat exchange with the flowing down desalinated water injected at the top of heat exchanger 114 at e.g. 370 C. (t the nitrogen flows out at the top of heat exchanger h4 through conduit 81, at e.g. 368 C. (11 starting a new nitrogen cycle.

The 23% of nitrogen per cycle exiting from heat exchanger h1 through tube a flows through conduit 101, manifold 102, stop valve 103 into the left cylinder chamber of compressor c4 including cylinder 104 and piston 105 connected to piston rod 6. At the same time the right cylinder chamber of compressor 04 acts as a compressor and a delivery chamber, where the nitrogen is compressed from 220 to 245 atmospheres, causing the rise of the temperature from e.g. 214 C. (t to e.g. 229 C. (i The compressed nitrogen is delivered through stop valve 106, manifold 107, conduit 108, regulating valve w2, conduit 109 and injector a' into heat exchanger h4, at about mid-way of its height, and also through regulating valve w'2, conduit 109' and injector b into heat exchanger h5 at about one-fourth of its height. About 20.7% or about 1.2 tons of nitrogen per cycle flows through regulating valve w2, and about 2.3% or about 0.13 ton of nitrogen per cycle flows through regulating valve w2. From the botom of heat exchanger 114 up to the level of tube a flows about 3.96 tons nitrogen, or about 69.3%, and from the level of tube a' flows up about 5.15 tons, or about of the total nitrogen per cycle. The work of compression of the 23%, or 1.32 tons of nitrogen from 220 to 245 atmospheres by compressor c4, is about 5.81 kwh.

(4) Temperatures, pressures and other data. The above temperature and other data figures, as well as the data in the tables below, are approximate with respect to the above described embodiment of the invention and are given by way of example only. The following data relate to the quantities in weight (tons or percent) and in volume (m. of the fluids mentioned in the above example, namely, sea water (SW), desalinated water (DW), saline brine (SB), nitrogen (N and parafiin (Pan), per cycle of 1.1 ton of incoming sea-Water. The fluids are compressed or expanded within and flow through the pumps P and P compressors c1, c2, c3 and c4, and prime movers M M M and M The theoretical Work needed and generated is in kwh. The temperatures (t.) are in C., and the pressure (p) in atmospheres. The notations (in) and (out) mean that the fluid flows into the pumps, compressors or prime mover, or flows out from same. The figures with respect to the volume of nitrogen are based on the pv table appearing in International Critical Tables, volume 3, page 17.

Pump compressor or Quantities of fluid prime Tempera- Pressure Work Fluid mover ture C.) (atms) Tons Percent mfi (kwh.)

SW (In) P1 17 1 1.125 1. l P 17 220 1. 100 1. 1 6. 77 01 395 220 1. 0 89 7. 7 01 410 245 1. O 89 7. 0 -5. 20 SB (111) 02 395 220 0. 125 11 SB (out) 02 405 245 0. 125 11 0. 21 M 30 245 1. 0 89 1. 0 M 30 1 1. 0 89 1. 0 +6. 86 M2 30 245 0. 125 11 0. 1 M2 30 1 0. 125 11 0. 1 +0. 69 c3 19 220 4. 4 77 18. 8 N2 (out) c3 28 245 4. 4 77 17. 7 12. 01 N2 (in) B4 214 220 1. 32 23 8. 6 229 245 1. 32 23 7. 9 6. 77 M4 383 245 5. 72 100 44. 8 M4 363 220 5. 72 100 48. 5 +37. 50 P; 358 220 4. 3 100 6. 5 Par. (out) P2 358 245 4. 3 100 6. 4 4. 53 Par. (1n) M3 403 245 4. 3 100 6. 7 Par. (out). M 403 220 4. 3 100 6. 8 +4. 7

The theoretical excess of work generated is approximately 13.40 kwh.

This theoretical excess of work generated is sufficient to guarantee the working of the pumps and compressors of the plant, assuming 85% average efiiciency for the the pumps, compressors and prime movers.

In the above described FIG. 2 embodiment of the present invention, all the mechanical work needed for the production of 1 ton of fresh water from 1.1 tons of saline water was produced by converting into mechanical power about 30 kwh. of heat energy (the heat of about 2.5 kg. of fuel, for instance) supplied to the system.

The amount of fuel heat to be supplied to the system could be reduced by working with a smaller pressure difference, for instance, instead of a pressure difference of 25 atmospheres as in the above described example. The cycle could be performed with a pressure difference of only atmospheres (at 220 and 235 atmospheres, for instance). In this case the rise of the temperature of the nitrogen by compression at 10 C. from 220 to 235 atmospheres will be about 6 C. (i.e. from 19 C. to C., for instance), instead of 9 C. in the above example. This means that the outfiowing fresh water and saline brine will be at a temperature lower by 3 C. than in the given example, which reduces the heat losses by the outflowing fresh water and saline brine.

Following is a recapitulation of the important (approximate) temperatures in the above described example:

t =17 C.temperature of the incoming saline Water.

t =19 C.lowes t temperature of the nitrogen cycle,

cooled by the incoming saline water at t t =28 C.temperature of 77% of nitrogen after compression from 220 to 245 atm.

t C.temperature of the outflowing desalinated water and saline brine.

t =200 C.intermediary temperature of the saline t =214 C.temperature of the cooled 22.5% of the nitrogen by saline water of 200 C.

t =229 C.temperature of 23% of the nitrogen after compression from 220 to 245 atm.

t =356 C.temperature of saline water heated by nitrogen at 21,.

t =358 C.lowest temperature of the parafiin cycle,

cooled by sea water at t =363 C.temperature of 100% of the nitrogen after expansion from 2 45 to 225 atm. at the highest temperature of the nitrogen cycle (r t =368 C.temperature of nitrogen heated by desalinated water at t t =370 C.temperature of desalinated water cooled by paraflin at t t =378 C.temperature of nitrogen heated by saline brine at about 405 C.

t =383 C.temperature of 100% nitrogen after heating by fuel heat from t =374 C.the critical temperature of the water.

l =395 C.temperature of saline water heated by paraffin at r and by fuel (by heating coil 19).

t =403 C.temperature of paraffin after heating by desalinated water vapor at the highest temperature of the system t t :4l0 C.the highest temperature of the desalinated water vapor obtained by compression at i from 220 to 245 atm.

In the above described embodiment of the invention, the improved method of converting thermal energy into motive power is utilized to produce all the mechanical work needed to operate the improved desalinization process. This improved method of converting heat energy into work could be performed for any other purpose, by using an intermediary fluid in the liquid state (e.g. water, as in the above described embodiment of the invention, or parafiin, or any liquid that is not miscible and does not react chemically with the gas used as power fluid), as a heat exchange medium between a cold and compressed fluid in the gaseous state (eg air or nitrogen) on the one hand, and the same gas, after expansion to a lower pres- 7 sure (the two pressures being substantially above one atmosphere) at a high temperature, on the other, the expanded gas being cooled by counter-current heat exchange and direct contact with cold water, for instance, to a little above ordinary temperature, while the water is being heated to a little below the temperature of the hot expanded gas. The so cooled gas is compressed and then heated in a first step by counter-current heat exchange with heated water, after being compressed, and in a second step by fuel heat. Finally the so heated compressed gas is allowed to expand, converting into useful work a substantial proportion of the heat energy supplied to the system, this feature enabling the attainment of a high thermal efficiency.

(5 Starting-up pr0cedure.-At the very beginning, the operation of the plant is started in the following manner:

(1) Pump P prime mover M and reservoir r;, are filled with liquid paraffin or any other liquid having the same needed properties (see above) through funnel and valve 111. All the valves of the apparatus are open, except for gas vent g and valves d, G G G G 51', 42, 25, 24, 15, 15' and 15", that are closed). When the filling up with paraffin is finished, valve 111 is closed.

(2) Water (saline water or preferably fresh water) is driven into the plant through valve 1 and conduit 1. When water starts to flow out through gas vent g it is closed; when water starts to flow out through valve 63, it is closed; and finally when water starts to flow out through vents g g g g and g they are also closed. At this moment all the receptacles and the conduits of the water cycle (except compressor 0 and prime mover M and the nitrogen cycle (see above) are completely filled with water.

(3) Valve 1' is closed (valves 113 and 114 are open), and a water cycle is operated by pump P starting from conduit 63 and driving the water through pump P heat exchangers I11 and 122 and coil 19 that is heated to about e.g. 400 C. The heated water continues to flow through tank s, compressor cl, heat-exchangers I13 and M, and finally through prime mover M and conduit 63 into pump P starting a new water cycle. By operating a number of cycles, the circulating water is gradually heated by the heating coil 19 to about 370 C., for instance, and the pressure is raised to about 220 atmospheres. Gas vents g g and g are regulated to a maximum pressure of 220 atmospheres, for instance, so that the additional volume of the water caused by the raise of the temperature escapes through these three safety valves.

(4) Nitrogen is driven into the plant at a pressure of 220 atmospheres by compressor c5. The nitrogen flows through pipe 115 connected to a nitrogen reservoir (not shown on the drawing), valve 116, compressor 05 (valve 84' is closed), valve 117, conduit 84, prime mover M into heat exchanger I11, through injector (1 (valve 15 is opened until about half of the water escapes and is replaced by nitrogen, and is then closed), then through conduits 92 and 101 into compressors c3 and c4, respectively, and into heat exchanger h4 (valve 63' is opened until about half of the water escapes from heat exchanger h4 and is replaced by nitrogen, and is then closed), then through conduit 81 and injector b into heat exchanger k5 (valve 15' is opened until about half of the water escapes and is replaced by nitrogen, and is then closed). At this stage valve 116 is closed (valves 117 and 118 are open), and the nitrogen is driven through the plant (see the nitrogen cycle) and through coil 83 heated to about 390 C. After a number of cycles the temperature of the nitrogen is raised to about 370 C.

The paraffin is driven from reservoir 13 into heat exchanger k2 by opening valve 119 and valves d and G The nitrogen flows into reservoir r3 through valve 119 and drives the paraflin through conduit 120, valve 66 prime mover M conduit 71, heating coil 19", injector a3, into heat exchanger I12 until half of the volume of the water is replaced by paralfin. Then valves d, 6,, and 66,, are closed. Then valves 121 and 80,, are opened and the parafiin flows from reservoir r3 through pipe 122, valve 80 conduit 80 and injector a'3 into heat exchanger h3 until half of the volume of the water is replaced by paraffin. Then valves 119, 121 and 80,, are closed.

(6) At this stage the operation of the plant is started as follows:

(a) Stop valves 86 and 89 of prime mover M are opened and stop valves 86 and 89 are closed (or vice versa).

(b) Valves 84', 116 and 117 are opened and valve 118 is closed, and compressor 05 drives into the plant an additional quantity of nitrogen to raise the pressure within heat exchangers h4 and k5 from 220 to 245 atmospheres, and to drive piston 88 of prime mover M from left to right together with all the other pistons connected by piston rod 6 (see above).

(c) Finally, valve 1' is opened to let in the saline water; valve 63 is opened to let out the produced fresh water; and valves 42 and 15" of the saline brine cycle are also opened.

(d) When the manometers on the safety valves g g and g indicate a pressure of 220 atmospheres and the manometers of the safety valves g g and g indicate a pressure of 245 atmospheres, and the movement of piston rod 6 has reached its normal speed, then compressor 05 is stopped and the apparatus works by the motive power generated from the heat energy supplied to the system by the heating coils 19, 19, 19" and 83. The safety valves are regulated to a maximum pressure of 300 atmospheres, for instance. Valves 84', 34, 36', 51' and 15 are open.

If the apparatus is stopped for a long time, then valves 16, 21, 36' and 34' are closed, and the parafiin is allowed to fiow into reservoir r3 by opening valves 66a, valve d, valve G valve 80b and gas vent g before the water within heat exchangers I12 and h3 is cooled and its specific gravity becomes greater than the specific gravity of the paraffin at the same temperature and pressure (see above). In such a case, all the water contained at the lower part of heat exchanges P12 and k3 is expelled through valves 6., and 121 respectively before collecting the paraffin into reservoir r3.

My invention permits the construction of desalination systems providing yields of 90% or more, which compares very favorably with prior known systems.

(6) Salt extraction.In the above examples the phase separation conditions are: pressure 220 atmospheres (227 kg./cm. and temperature 395 C. If without changing the pressure of 220 atmospheres, the temperature in heat exchanger I12 is raised to a little below the saturation temperature of the sodium chloride (428 C.) and then the mixture flowing into tank s is heated above 428 C., the salts are precipitated in tank s and are collected in the cells 23 and 24. The precipitated salts could be evacuated together with a little of the mother brine in any known intermittent or continuous manner from the cells 23 and 24.

(F) THE IMPROVED EMBODIMENT OF FIG. 3

FIG. 3 illustrates a further embodiment of the inven tion incorporating several improved features, and particularly the hydraulic devices illustrated in detail in FIGS. 4-7. For the sake of simplifying the description, many of the control valves and other accessories that would normally be included in the system are omitted from this figure.

To facilitate understanding the diagram of FIG. 3, the saline water paths are shown in heavy lines, the desalinated or pure water (or vapor) paths are shown in double lines, the paraffin paths are shown in thin lines, the nitrogen paths are shown in dashalash lines, and the brine and crystallized salt paths are shown in dot-dot lines.

(1) Water cycle.The raw saline water SW at normal temperature and pressure is drawn from the reservoir R1, such as the ocean, through line 502 to a hydraulic system SD, illustrated and described below with respect to FIG. 7. The hydraulic system SD boosts the pressure of the saline water to about 225 kg./cm. and passes it through line 504 to reservoir R2. The latter reservoir is closed so that the pressure therein is the same as in line 504. From reservoir R2, the saline water flows into the top of a heat-exchanger H1.

Heat-exchanger H1, as those in FIG. 2 and the others to be described, is of the counter-current direct contact type, preferably as described in my pending US. patent application Ser. No. 346,953, filed Feb. 24, 1964.

In heat-exchanger H1, the saline water is heated by hot up-fiowing nitrogen, as will be described below in detail, and leaves the heat-exchanger through line 508 at a temperature of something less than the phase separation temperature of the saline water, preferably between about 260 C. and 360 (3., depending upon the particlar design. The pressure of the saline water as it leaves heat-exchanger H1 is about 225 kg./cm.

The saline water is then passed through a small compressor C1 where its pressure is boosted to about 226 kg./cm. and is introduced through line 510 into heatexchanger H2. Here, the saline water is heated by down flowing hot paraffin, and also by a little steam, both of which will be described below in connection with their respective cycles, and leaves heat-exchanger H2 through line 512 at a temperature above the critical temperature (374 C.) but below the saturation temperature of the dissolved salts (428 C. for sodium chloride). The temperature of the water vapor at the critical pressure leaving heat-exchanger H2 through line 512 would preferably be in the order of 400 C.

Water solution-water vapor phase separation occurs in heat-exchanger H2 inasmuch as the saline water is heated to below the saturation temperature. Accordingly, this heat-exchanger will contain quantities of: (a) an upflowing saline liquid having an increasing concentration, being a concentrated brine a little below the top of the heat-exchanger; (b) the separated water vapor, which increases in volume from bottom to top; (c) down-fiowing parafiin; and ((1) small quantities of calcium carbonates and sulfates mostly entrained from H1. The water vapor rises to the top and flows out through line 512. The concentrated brine is drawn off at a lower level; the parafiin settles at a little above the bottom; and a part of the calcium carbonates and sulfates, and other solids that cannot exist in a water solution at these temperatures, settle at the bottom of heat-exchanger below the paraffin. The removal of these substances from heat-exchanger H2, and their further handling in the system, will be described belowhin connection with the description of the cycle of eac The heated saline water and vapor passing through line 512 are introduced into the bottom of a tank S1, which functions as a third heat-exchanger and vapor washing and filtering device, for further heating to a temperature of about 432 C. (over the saturation temperature) by means of down-flowing paraffin. The phase separation of the saline water and the washing and filtering of the separated water vapor are thus completed in tank S1. In addition to the relatively pure water vapor, tank S1 includes entrained small drops of concentrated brine, parafiin, and crystallized salt, all of which are removed in the manner to be described more fully below. The water vapor is removed from tank S1 through line 514- where its temperature is 432 C. or higher, and its pressure is about 226 kg./cm.

From line 514, the water vapor passes into hydraulic pressure-exchanging device A2-B2 (having the same structure as A4-B4 illustrated in FIG. 6 described below) where its pressure is boosted to about 245 kg./cm. and its temperature to about 446 C., and leaves this device through line 516.

It is in pressure-exchanger A2-B2 that the additional compression takes place in this embodiment to overcome the squeeze problem previously discussed with respect to FIG. 1.

From line 516, the water vapor is passed through a heater F1 where its temperature is boosted to about 460 C. raising the enthalpy from 705 to 721 kcal./kg. (but this may vary, depending upon the amount of heat added at other points in the circuit, as will be described later), and is then introduced into heat-exchanger H3 through line 518.

In heat-exchanger H3, the water vapor heats paraffin applied from several locations along the length of the heat-exchanger and eventually exits therefrom through line 520 at a temperature somewhat below the critical temperature of the water, for example at some point in the range of 270370 C. The pressure of the now condensed and desalinated water in line 520 is still approximately 245 kg./cm.

The desalinated water then passes through hydraulic pressure-exchanger A3-B3, the structure of which is illustrated in FIG. 5 described below, and exits therefrom through line 522 at a pressure of about 255 kg./cm. and is then introduced at the top of heat-exchanger H4.

In pressure-exchanger A3B3, additional compression takes place which is a further feature of this embodiment as will be more fully described below.

In heat-exchanger H4, the down-flowing desalinated water heats up-fiowing nitrogen and exits through line 524 at a temperature of about 37 C. and pressure of about 255 kg./cm. into reservoir R3, which is pressurized at the same pressure as the water in line 524.

Reservoir R3 may be considered as part of the hydraulic system SD since its pressure is used to pump the saline water SW from line 502 into heat-exchanger H1 through line 504. This system is fully illustrated in FIG. 6 and is described in detail below. Suffice it to bring out at this point that the desalinated water from reservoir R3, after passing through system SD, eventually passes through line 698 into a reservoir R4 which is open to the atmosphere and therefore at atmospheric pressure. The water in reservoir R4 is available through outlet 526 and is substantially pure to be used for drinking, irrigation, and similar purposes. A small portion of the pure water is pumped back from reservoir R4 into the SD system through line 708, as will be described later.

(2) Nitrogen cycIe.-Now will be described the nitrogen cycle in which hot nitrogen heats cold saline water in heat-exchanger H1, and cold nitrogen is heated by hot desalinated water in heat-exchanger H4.

Reservoir R2 is in the nitrogen cycle, it being recalled that this reservoir is closed and contains the cold saline water at a pressure of about 225 kg./cm. The saline water settles at the bottom of the reservoir, and the top is filled with the nitrogen.

From reservoir R2, the nitrogen, at a temperature of about 22 C. and a pressure of 225 kg./cm. passes through line 528 into hydraulic pressure-exchanger device A4B4, illustrated in detail in FIG. 6. In the latter device its pressure is boosted to about 255 kg./cm. and its temperature to about 32 C. It then passes through line 530 into the bottom of heat-exchanger H4.

In heat-exchanger H4, the nitrogen is heated to a temperature in the order of 260360 C., depending upon the design, and exits from the heat-exchanger through line 532 at a pressure still about 255 kg./ cm. From line 532, the nitrogen then takes four different paths.

The first path of the nitrogen is through line 534 into pressure-exchanger A4B4, where its high pressure of about 255 kg./cm. is used to boost the pressure of the nitrogen coming through line 528 from about 255 kg./cm. to about 255 kg./cm. the latter exiting at line 530 and passing into heat-exchanger H4. The nitrogen from line 534, after passing through pressure-exchanger A4-B4, drops in pressure to about 225 and is then compressed to about 255.5 l g./cm. (by compressor C8 in FIG. 6) and exits from the latter device through line 536. As indicated earlier, the structure of pressure-exchanger A2- B2 is the same as that of A t-B4 illustrated in FIG. 6.

The nitrogen from line 536 passes into line 538, which is a common line for the return of all the nitrogen from the above-mentioned four paths from heat-exchanger H4. This nitrogen is reintroduced into heat-exchanger H1 through line 538 for heating the saline water and exits from the heat-exchanger through line 540 into reservoir R2.

The second path of the nitrogen exiting from heatexchanger H4- through line 532 includes line 542 directing the nitrogen into pressure-exchanger A3B3, the structure of which is illustrated and described below in connection with FIG. 5. In this pressure-exchanger, the nitrogen at a pressure of about 255 kg./cm. is used to boost the pressure of the desalinated water from about 245 kg./cm. to about 255 kg./cm. the latter exiting through line 522. The nitrogen exits from pressure-exchanger A3-B3 through line 544 at a pressure of about 245 kg./cm.

The nitrogen then passes through turbine T1 and exits from that turbine through line 546 to common return line 538 at a pressure of about 225.5 kg./cm. The drop of pressure of the nitrogen in turbine T1, from 245 kg./ cm. to 225.5 kg./cm. produces a mechanical output in the turbine which may be used for driving the various pumps and compressors in the system. This will be more fully described below in connection with the description of the other turbines which are also driven by the expanding nitrogen to produce a mechanical output for driving the pumps and compressors.

The third path of the nitrogen from heat-exchanger H4 and line 532 includes line 548 where it is directed through turbine T2, exiting therefrom through line 550 and then into pressure-exchanger A2B2. In turbine T2, the pressure of the nitrogen drops from 255 kg./cm. to about 245.5 kg./cm. this drop in pressure also being used by means of the turbine to produce a mechanical output for driving pumps and compressors. In the pressureexchanger A2-B2 the work of the in-fiowing nitrogen at a pressure of 245.5 l g./cm. is used to boost the pressure of the water vapor from tank S1 (through line 514) as briefly described below, from 226 to 245 kg./cm. and to drive out the same through line 516, heating coil F1 and line 518 into the bottom of heat exchanger 43. Pressure-exchanger A2B2 is the same as A4-B4 illustrated in detail in FIG. 6.

From pressure-exchanger A2B2, the nitrogen at a pressure of about 225.5 kg./cm. then passes through conduit 552 into line 538, joining with the nitrogen from the other paths for introduction into heat-exchanger H1.

The fourth path of the nitrogen from heat-exchanger H4 through line 532 includes line 554 where it passes through turbine T3 exiting from the turbine through line 556 into common line 538. In turbine T3, the pressure of the nitrogen drops from about 255 kg./cm. to 225.5 kg./ cm.', this drop in pressure also being used to produce a mechanical output for driving the pumps and compressors.

This completes the description of the nitrogen cycle, except for a very minor cycle which will be described later.

With respect to the relative amount of nitrogen that may be diverted to each one of the above four paths, following is one example based upon a total quantity of nitrogen of 4,100 kg. per cubic meter of water produced, this being in volume about 32,500 litres under the conditions it exists when exiting from heat-exchanger H4: In the first-mentioned path, to compress the nitrogen in pressure-exchanger A4434, about 18,500 litres of nitrogen is used. In the second-mentioned path, to compress the desalinated water in pressure-exchanger A3B3 and to drive turbine T1, about 1400 litres of nitrogen is used. In the third-mentioned path to drive turbine T2 and to compress the steam in pressure-exchanger A2-B2, about 11,200 litres of nitrogen is used. This leaves about 1,400 litres of nitrogen available for the fourth-mentioned path to drive turbine T3.

The output of these three turbines is available for doing mechanical work in the plant, for example, for driving the compressors, pumps, cyclic valves, etc. This is schematically indicated in FIG. 3 by the mechanical coupling 557 shown in broken dash-dot lines leading from the turbines to some (not all, for the sake of simplicity) pumps and compressors. Eventually the excess of mechanical work that may be obtained could be utilized for any purpose external to the system.

(3) Parafiin cycle.Now will be described the paraffin cycle in which the parafin heats the saline water in heat-exchanger H2 and is in turn heated by the desalinated water in heat-exchanger H3.

Starting with line 558 where the hot parafiin is introduced into heat-exchanger H2, the down-flowing paraffin in this heat-exchanger heats the saline water applied through line 510. The input temperature and pressure of the hot parafiin in line 558 are about 400450 C., and 226 kg./cm. respectively. The paratfin leaves heatexchanger H2 through two lines, 560 and 562, the temperature of the paraflin in the latter being lower.

Heat-exchanger H2 is basically of the counter-current direct contact type as the other heat-exchangers but preferably includes the baffle arrangement to be described below.

It will be recalled that the saline water is introduced into heat-exchanger H2 through line 510 at a temperature which might be in the range of 280 C.350 C. At the lower part of this temperature range, the saline water is heavier than the paraffin. Accordingly, at this part of the temperature range, both the saline water and the paraffin will flow in the same direction, i.e., downwardly, in direct heat-exchange contact.

In the case where the water is introduced at this lower part of the temperature range, an open-bottom concavetype annular bafile 564 is interposed, and there-below are also interposed an open-top, convex-type annular bafi'le 566, and an open-top concave-type annular bafiie 567. The arrangement is such that the down-flowing saline water and the down-flowing paraflin will be in direct contact with each other as they pass through the inside of bafiie 564, the outside of baffle 566, and the top (or outside) of bafiie 567, the paraffin all the while heating the saline water. When both reach the top of bafi le 567, the saline water is heated to a sufficient temperature where it is now lighter than the paraffin at the same region, and therefore the saline water will pass through the inside of baffie 566. Through its open top, and will continue upward through the heat-exchanger H2, all the while being further heated by the downfiowing paraflin.

Such a bafiie arrangement makes it possible to use two cycles of parafiin for the whole process: one for the higher temperature range as described above and the other for the temperature range between ordinary temperature and about 300C.

As indicated earlier, the greatest portion of the phase separation occurs in heat-exchanger H2, and therefore this heat-exchanger will contain incoming saline water, water vapor, concentrated brine, parafiin, and crystallized calcium sulfates and carbonates. The densities of these substances are such that they settle and leave the heatexchanger in the following manner:

The water vapor will rise to the top of the heat-exchanger and leave it through line 512, as described earlier.

The concentrated brine will rise to a level just above an outlet line 568, and will therefore be drawn out through that line. At this level in heatexchanger H2, a settling tank S2 is provided together with a cover 569 thereover, to exhaust the brine and to shield the settling tank from the down-flowing paraffin. The brine leaving heat-exchanger H2 through line 568 flows into a further heat-exchanger H5 (not yet described) for separating all or almost all the water contained in the brine, for crystallizing the salt in the brine, and also for utilizing some of its heat to pre-heat the nitrogen. The water removed from the brine in heat-exchanger H5 is returned through line 570 into heat-exchanger H2 in the form of high-temperature steam, as will also be described below.

Heat-exchanger H2 also preferably includes a plurality of screens (not shown) at the top thereof and overlying settling tank S2 and its cover 569 and arranged in a criss-cross pattern, but spaced in between each. These screens, when used, would be in the path of the down-flowing parafiin and would therefore be coated by it. They would also be in the path of the up-flowing water vapor, and accordingly the latter would be continuously washed by the paratfin of any brine drops entrained with the vapor.

The paraflin removed from heat-exchanger H2 through line 560 is caught by a funnel 572 interposed at an intermediate point in the heat-exchanger. From line 560 the parafiin, at a pressure of about 226 kg./cm. passes through a hydraulic pressure-exchanger A5-B5, the structure of which is illustrated in FIG. 4 and will be described below in detail. The paraffin leaves pressure-exchanger AS-BS through line 574 at a pressure of about 245.5 kg./cm. and is introduced into heat-exchanger H3 where it is heated by the up-flowing hot desalinated water vapor.

Paraffin leaves heat-exchanger H3 through funneled outlet line 576. Part of it passes back through pressureexchanger AS-BS where its pressure is dropped from 245 kg./cm. back to about 226 kg./cm. exits from the pressure-exchanger through line 578, passes through a heater coil F2 where its temperature is further raised, and then back into line 558 for introduction into the heat-exchanger H2.

The parafiin leaving heat-exchanger H2 through line 562 is withdrawn from the heat-exchanger at a lower level than that leaving the heat-exchanger through line 560, and therefore at a lower temperature. This parafiin is directed through pressure-exchanger A6-B6 (which is of the same construction as pressure-exchanger A5B5) where its pressure is boosted from 226 kg./cm. to about 245.5 kg./cm. The parafiin leaves the latter pressureexchanger through line 580 and is introduced into heatexchanger H3 for heating by the up-fiowing hot desalinated water vapor. This paraflin is also removed from the heatexchanger through funneled outlet line 576 where it joins with the paraflin introduced through line 574. Part passes through line 581, pressure-exchanger A6-B6, line 582 to line 578, and the remainder passes through pressure-exchanger AS-BS to line 578, and from there through heating coil F2 and line 558 for reintroduction into heat-exchanger H2.

There is a minor parafiin cycle which includes heatexchanger H3 for heating the water vapor in tank S1. In this minor paraffin cycle, the paraifin is introduced into heat-exchanger H3 through inlet line 583 at a point below the funneled outlet line 576 of the earlier described parafiin cycle. It leaves the heat-exchanger H3 through line 584, and passes through a further pressure-exchanger device A7B7, which is the same type of system as pressure-exchanger devices A5-B5 and A6B6. In pressure-exchanger A7B7 the paraflin pressure is dropped from 245 kg./cm. at line 584 to about 226 kg./cm. at the exit line 586 and is introduced into tank S1. 

